US6241952B1 - Countercurrent reactor with interstage stripping of NH3 and H2S in gas/liquid contacting zones - Google Patents

Countercurrent reactor with interstage stripping of NH3 and H2S in gas/liquid contacting zones Download PDF

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US6241952B1
US6241952B1 US09/373,255 US37325599A US6241952B1 US 6241952 B1 US6241952 B1 US 6241952B1 US 37325599 A US37325599 A US 37325599A US 6241952 B1 US6241952 B1 US 6241952B1
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reaction zone
gas
reaction
liquid
reactor
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Edward S. Ellis
Ramesh Gupta
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ExxonMobil Technology and Engineering Co
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Exxon Research and Engineering Co
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G49/00—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00
    • C10G49/002—Apparatus for fixed bed hydrotreatment processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
    • B01J8/0492—Feeding reactive fluids

Definitions

  • the present invention relates to a reactor for reacting liquid petroleum or chemical streams wherein the liquid stream flows countercurrent to the flow of a treat gas, such as a hydrogen-containing gas.
  • the reactor is comprised of at least one vertically disposed reaction zone, each containing a bed of catalyst, wherein each reaction zone may contain vapor bypass means, and wherein each reaction zone is immediately preceded by a non-reaction zone, and wherein each non-reaction zone contains a gas/liquid contacting zone for stripping gaseous by-products, such as NH 3 and H 2 S, from the liquid stream.
  • U.S. Pat. Nos. 3,767,562 and 3,775,291 disclose a similar process for producing jet fuels, except the jet fuel is first hydrodesulfurized prior to two-stage hydrogenation.
  • U.S. Pat. No. 5,183,556 also discloses a two-stage concurrent-countercurrent process for hydrofing—hydrogenating aromatics in a diesel fuel stream.
  • the distillation apparatus which is a vessel, contains vapor passageways which provide a means for vapor communication between fractionation sections located above and below catalyst beds. Substantially all of the vapor in the vessel rises through the vapor passageways and the desired contacting between vapor and liquid occurs in the fractionation sections.
  • Reaction vessels have been disclosed in co-pending U.S. patent applications Ser. No. 08/855,699, now U.S. Pat. No. 5,939,031; and 08/885,788now U.S. Pat. No. 5,942,197; both entitled “Countercurrent Reactor”, and both filed Jun. 30, 1997, and both of which are incorporated herein by reference.
  • These two co-pending applications disclose countercurrent reactors which are less susceptible to flooding than conventional countercurrent reaction vessels. This is primarily due to the novel use of vapor passageways which act to selectively bypass a fraction of the upward-flowing treat gas through one or more of the catalyst beds.
  • bypass tubes provide a great improvement in countercurrent reactors, there is still a need in the art for further improvement, particularly for improving the liquid flow rate through the reaction beds of a countercurrent reactor. There also exists a need for improved countercurrent reaction vessel designs which are not as readily susceptible to flooding, or which can more easily recover without shutdown should flooding occur.
  • a reactor for reacting liquid petroleum and chemical streams with a hydrogen-containing treat gas in the presence of a catalyst in at least one countercurrent reaction zone which reactor comprises:
  • gas bypass means in said first reaction zone for allowing a portion of the treat gas to bypass said first reaction zone.
  • the reaction vessel contains a plurality of said reaction zones and wherein there is a non-reaction zone immediately upstream of each reaction zone and wherein each non-reaction zone contains a gas-liquid contacting zone containing a contacting means.
  • the reaction vessel contains a plurality of said reaction zones and said vapor bypass means are such that they allow treat gas to by pass all of said reaction zones with fresh treat gas introduced below each said reaction zone, or below each said contacting zone.
  • the contacting means is comprised of open-structure solid material selected from Raschig rings, Intalox saddles, Pall rings, Berl saddles, Cyclohelix spiral rings, Lessing rings, and Cross-partition rings.
  • At least one of the vapor passageways is external to the reaction vessel.
  • FIG. 1 hereof is one embodiment of the present invention which shows a reactor having three reaction zones, each of which contains vapor bypass tubes so that a portion of the upflowing vapor can bypass the reaction zones, and contact downflowing liquid in the gas/liquid contacting zones upstream of each reaction zone.
  • FIG. 2 is a representation of another embodiment of the reactor of the present invention wherein treat gas and gaseous impurities from the liquid stream are passed directly to the gas outlet of the reactor. Also shown is fresh treat gas being introduced downstream (with respect to the flow of liquid) of each gas/liquid contacting zone.
  • the reactors of the present invention are suitable for use in any petroleum or chemical process wherein it is advantageous to pass a gas, such as a hydrogen-containing treat gas, countercurrent to the flow of liquid feedstock.
  • a gas such as a hydrogen-containing treat gas
  • refinery processes in which the instant reaction vessels can be employed include the hydroconversion of heavy petroleum feedstocks to lower boiling products; the hydrocracking of distillate boiling range feedstocks; the hydrotreating of various petroleum feedstocks to remove heteroatoms, such as sulfur, nitrogen, and oxygen; the hydrogenation of aromatics; and the hydroisomerization and/or catalytic dewaxing of waxes, particularly Fischer-Tropsch waxes.
  • the reaction vessels of the present invention be those in which a hydrocarbon feedstock is hydrotreated and hydrogenated, more specifically when heteroatoms are removed and when at least a portion of the aromatic fraction of the feed is hydrogenated.
  • the treat gas which typically flows upward through the bed of catalyst comprising a reaction zone, hinders the downward movement of the liquid.
  • the hindrance from the upward moving gas is not enough to cause flooding and the liquid in the reaction vessel is able to drain through the catalyst bed or beds.
  • the upflowing gas rate, or the downflowing liquid rate is too high, liquid cannot drain through the catalyst bed. This is known as “flooding.”
  • the liquid holdup in the catalyst bed increases and liquid may begin to accumulate above the top surface of the catalyst bed.
  • the upflowing gas rate at which flooding occurs in a given bed will depend on such things as the rate and physical properties of the downflowing liquid.
  • the downflowing liquid rate at which flooding occurs in a given bed similarly depends on the rate and properties of upflowing gas.
  • reactors with vapor passageways provide a somewhat self-adjusting regulation of upward-flowing vapor, thereby extending the hydrodynamic operating window of the reaction vessel. Further extension of this range can be provided by including one or more external vapor passageways with flow control means.
  • Such a system provides a means by which catalyst bed pressure drop, and therefore catalyst contacting efficiency, can be controlled.
  • the external vapor passageways can be controlled with a control means, preferably a valve for so-called “trim” bypassing.
  • the valve can be automatically controlled so that it opens and closes to the appropriate degree in response to a signal transmitted in response to pressure drop changes in the catalyst bed(s). That is, the trim bypass will be used to keep the reaction vessel operating as close to flooding as desirable.
  • Treat gas which bypasses a particular catalyst bed or beds may pass through the other catalyst bed(s) and serve to take part in the desired hydroprocessing reactions, carry away light or vaporized reaction products, strip catalyst poisons such as hydrogen sulfide, water and/or ammonia, etc.
  • the gas bypassing may also be self regulated using the invention described in co-pending U.S. patent application Ser. No. 08/885,788 filed on Jun. 30, 1997.
  • the vapor passageways provide an extended operating range and an opportunity to operate close to the flooding point of the reaction vessel. This enables a more stable, more efficient reaction vessel operating regime. Further, the reaction vessel can safely and continuously operate while responding to normal process fluctuations in liquid and vapor flow rate and temperature. The range of total flow rates that can be tolerated is thereby extended. Operating close to the flooding point results in relatively efficient contacting because the catalyst particles are well irrigated by the downflowing liquid. In the absence of vapor passageways, a conventional countercurrent reaction vessel would need to operate at lower efficiency in order to remain operable.
  • downstream and upstream are with respect to the flow of liquid which will typically flow downward.
  • the reaction vessels of the present invention provide vapor bypass means such that substantially all of the treat gas from a downstream (with respect to the flow of liquid) gas-liquid contacting zone can bypass the catalyst beds of the reaction zones without a significant decrease in reaction activity or selectivity.
  • a preferred feedstock can be used which contains enough dissolved hydrogen to satisfy demand for hydrogen in the catalyst bed, such that substantially all of the treat gas can be made to by-pass at least one of the reaction zones. This allows for substantially greater liquid flow rates through reaction zones, when compared to other countercurrent reactors. This is accomplished by providing a gas/liquid contacting zone immediately before and immediately after each reaction zone.
  • the gas/liquid contacting zone contains suitable gas/liquid contacting material and greatly enhances the removal of undesirable reaction products, such as NH 3 and H 2 S from the downflowing feed stream, while providing the desired saturation of the liquid with dissolved treat gas components, such as hydrogen.
  • the primary function of the open structure packing is to facilitate the stripping of H 2 S and NH 3 from the downflowing liquid. While the open structure packing material will generally have very little or no catalytic activity, it should be understood that the same catalytic activity can also be imparted to the open structure material. In other words, the contacting zone may also use material having catalytic activity.
  • FIG. 1 shows reactor 1 which is generally comprised of a continuous wall 2 which encloses at least one reaction zone R 1 having a catalyst bed 4 suitable for causing a desired reaction between a liquid feedstock and a treat gas.
  • reaction zones R 1 , R 2 , and R 3 are shown serially disposed in the reactor of FIG. 1, the number of reaction zones will depend upon the particular needs of the reaction, as will be explained further herein.
  • Each reaction zone contains a bed of catalyst and is immediately preceded by a non-reaction zone NR 1 , NR 2 , NR 3 .
  • Each non-reaction zone contains a gas/liquid contacting zone CZ 1 , CZ 2 , CZ 3 , which contains an effective gas-liquid contacting means.
  • effective gas-liquid contacting means means a solid material having an effective surface area that will allow enough gas/liquid contacting to strip at least about 90 wt. %, preferably at least about 95 wt. %, of the trapped gases from the liquid stream.
  • Preferred solid materials that can be used in the gas-liquid contacting zone are open structured materials.
  • the stripped gases will typically be undesirable reaction products, such as NH 3 and H 2 S, which are produced while the feedstream is reacted in the reaction zones.
  • open-structured we mean that there is enough space either between or within the solid material so that the downflow of liquid is not significantly impeded.
  • the precise amount and size of the open-structure material must be balanced so that adequate surface area is provided for stripping and the flow of the liquid stream is not substantially reduced.
  • Non-limiting examples of gas-liquid contacting structures suitable for use in the reactors of the present invention include metallic and ceramic trays, as well as conventional packing shapes, such as Raschig rings, Intalox saddles, Pall rings, Berl saddles, Cyclohelix spiral rings, Lessing rings, Cross-partition rings, and the like.
  • These open-structures, which also include trays, provide adequate surface area for gas/liquid contact and the removal of the desired amount of gases from the downflowing liquid stream.
  • the downflowing liquid stream will still contain enough dissolved hydrogen after being stripped in an upstream gas/liquid contacting zone to enable the desired hydroprocessing reaction to occur. That is, a reaction wherein the consumption of hydrogen in the reaction zone is less than the amount dissolved in the incoming liquid.
  • substantially all of the treat gas can be made to by-pass at least one of the reaction zones. If the dissolved hydrogen in the liquid is not enough to meet the hydrogen demand due to the reaction, then all of the treat gas may not bypass the reaction zone.
  • Liquid inlet means 6 is located near the top of the reactor 1 and allows a liquid feed such as a feedstock to be treated, to enter the reactor 1 .
  • Gas inlet means 8 is located near the bottom of reactor 1 and allows treat gas to enter the reactor 1 .
  • Liquid outlet means 10 is located near the bottom of the reactor 1 and allows the reacted liquid stream to exit as a reaction product.
  • gas outlet means 12 is located near the top of the reactor 1 and allows treat gas to exit the reactor.
  • gas bypass means 14 are disposed through each reaction zone to enable treat gas to bypass at least one reaction zone.
  • the gas bypass means are comprised of one or more gas bypass tubes. Each gas bypass tube enables fluidic communication of the treat gas between two separate nonreaction zones.
  • FIG. 2 hereof shows an alternative embodiment of the reaction vessels of the present invention.
  • the reactor of this FIG. 2 is similar to that of FIG. 1 except that: (a) a portion of the fresh treat gas is introduced prior to each reaction zone at G 1 , G 2 , G 3 ; and (b) all treat gas, after passing through a gas/liquid contacting zone exits the reactor thereby bypassing more than one reaction zone, non-reaction zones, and downstream (with respect to the flow of treat gas) gas-liquid contacting zones through bypass tubes 16 and 18 . All other features of the reactor of FIG. 2 are identical to that of FIG. 1 hereof, and thus need not be shown.
  • the reaction vessels used in the practice of the present invention are operated at suitable temperatures and pressures for the desired reaction.
  • typical hydroprocessing temperatures will range from about 40° C. to about 450° C. at pressures from about 50 psig to about 3,000 psig., preferably 50 to 2,500 psig.
  • the liquid feedstock enters the reactor via line 6 and passes downward through gas/liquid contacting zone CZ 1 wherein at least a portion of any dissolved gases are separated from the feedstock and exit the reactor via line 12 with any unreacted treat gas and gaseous reaction products from downstream reaction zones.
  • the feedstream then passes through the catalyst bed of reaction zone R 1 where it reacts with dissolved hydrogen on the catalyst surface.
  • the reacted liquid stream, and any dissolved vapor-phase reaction products, are passed downward to non-reaction zone NR 2 which contacts upflowing treat gas in gas/liquid contacting zone CZ 2 .
  • At least a portion of the separated gases which now become part of the upflowing treat gas stream flow upward through bypass tubes 14 avoiding contact with the catalyst of reaction zone R 1 , and into non-reaction zone NR 1 where they contact the downflowing fresh feed stream in gas/liquid contacting zone CZ 1 where any undesirable gases from upstream processing of the stream are stripped.
  • the undesirable gases and treat gas then exit the reactor at gas outlet 12 .
  • This flow scheme is repeated as the reacted feed stream flows to downstream reaction zones and non-reaction zones.
  • vapor bypass means means
  • vapor passageways means
  • vapor passageway means vapor bypass tubes
  • gas bypass means are used interchangeably herein.
  • the vapor bypass tubes used in the practice of the present invention may be comprised of any material that can withstand the operating conditions of the reactor. Suitable materials include metals, such as stainless and carbon steels; ceramic materials; as well as high performance composite materials such as carbon fiber materials. Preferred are tubular passageways having round cross sections.
  • the tubes need not be perfectly vertical. That is, they can be inclined or curved, or even in the form of a spiral. It is to be understood that the passageways can be of any suitable size depending on the amount and rate of vapor one wishes to bypass from one non-reaction zone to another.
  • one or more of the bypass tubes can have a flat substantially horizontal member, such as a baffle, above it to prevent liquid from an upstream bed from falling into the passageways.
  • more than one bypass tube can be extended through any given reaction zone to enable substantially all of the treat gas to bypass that reaction zone.
  • One or more vapor bypass tubes can also be routed external to the reaction zone.
  • a tubular arrangement can be used on the outside of the reaction vessel so that one or more non-reaction zones are in fluid communication with any one or more other non-reaction zones.
  • the vapor bypass tubes may contain a flow control means to control the portion of vapors which is passed from one non-reaction zone to another non-reaction zone. If the vapor bypass tubes are external to the reaction vessel, then it is preferred that the flow control means be simply a flow control valve.
  • the vapor passageways bypass two or more catalyst beds, or reaction zones, as shown in FIG. 2 hereof.
  • the vapor passageways need not be hollow structures, such as solid-walled tubes, but they may contain a packing material, such as inert balls, or catalyst particles, or both. If catalyst particles compose at least a portion of the packing material in the vapor passageways, they can be used to further react the vapor phase reactants.
  • the packing material and/or catalyst particles in the vapor passageways can be of a different size than the catalyst particles in the catalyst beds of the reaction zones. Such packing may help to improve the bypassing characteristics of said tubes.
  • one or more co-current reaction zones be located upstream of one or more countercurrent reaction zones.
  • the co-current/countercurrent zones can be in separate vessels or in the same vessel. It is preferred that all countercurrent zones be in the same vessel.
  • Feedstocks treated by the practice of the present invention will most likely contain undesirable heteroatoms, such as sulfur and nitrogen.
  • one or more co-current reaction zones be upstream of the first countercurrent reaction zone. That is, it may be preferred that the upstream co-current reaction zone be one in which both a hydrogen-containing treat gas and the feed stream flow downward through a fixed-bed of suitable hydrotreating catalyst.
  • hydrotreating refers to processes wherein a hydrogen-containing treat gas is used in the presence of a catalyst which is primarily active for the removal of heteroatoms, such as sulfur, and nitrogen with some hydrogenation of aromatics.
  • hydroprocessing includes hydrotreating, but also includes processes which are primarily active toward the hydrogenation, hydrocracking, and hydroisomerization. Ring-opening, particularly of naphthenic rings, for purposes of this invention can also be included in the term “hydroprocessing”.
  • Suitable hydrotreating catalysts for use in the present invention are any conventional hydrotreating catalyst and includes those which are comprised of at least one Group VIII metal, preferably Fe, Co and Ni, more preferably Co and/or Ni, and most preferably Co; and at least one Group VI metal, preferably Mo and W, more preferably Mo, on a high surface area support material, preferably alumina.
  • hydrotreating catalysts include zeolitic catalysts, as well as noble metal catalysts where the noble metal is selected from Pd and Pt. It is within the scope of the present invention that more than one type of hydrotreating catalyst be used in the same reaction vessel.
  • the Group VIII metal is typically present in an amount ranging from about 2 to 20 wt. %, preferably from about 4 to 12%.
  • the Group VI metal will typically be present in an amount ranging from about 5 to 50 wt. %, preferably from about 10 to 40 wt. %, and more preferably from about 20 to 30 wt. %. All metals weight percents are on support. By “on support” we mean that the percents are based on the weight of the support.
  • Typical hydrotreating temperatures range from about 100° C. to about 400° C. with pressures from about 50 psig to about 3,000 psig, preferably from about 50 psig to about 2,500 psig. If the feedstock contains relatively low levels of heteroatoms, then the co-current hydrotreating step may be eliminated and the feedstock passed directly to an aromatic saturation, hydrocracking, and/or ring-opening reaction zone.
  • hydrogen-containing treat gas means a treat gas stream containing at least an effective amount of hydrogen for the intended reaction.
  • the treat gas stream introduced to the reaction vessel will preferably contain at least about 50 vol. %, more preferably at least about 75 vol. % hydrogen. It is preferred that the hydrogen-containing treat gas be make-up hydrogen-rich gas, preferably hydrogen.
  • the liquid phase in the reaction vessels used in the present invention will typically be the higher boiling point components of the feed.
  • the vapor phase will typically be a mixture of hydrogen-containing treat gas, heteroatom impurities, and vaporized lower-boiling components in the fresh feed, as well as light products of hydroprocessing reactions. If the vapor phase effluent still requires further hydroprocessing, it can be passed to a vapor phase reaction zone containing additional hydroprocessing catalyst and subjected to suitable hydroprocessing conditions for further reaction. It is to be understood that all reaction zones can either be in the same vessel separated by non-reaction zones, or any can be in separate vessels. The non-reaction zones in the later case, can be the transfer lines containing gas-liquid contacting material leading from one vessel to another.
  • a feedstock which already contains adequately low levels of heteroatoms be fed directly into a countercurrent hydroprocessing reaction zone for aromatic saturation and/or cracking.
  • a preprocessing step is performed to reduce the level of heteroatoms, the vapor and liquid can be disengaged and the liquid effluent directed to the top of a countercurrent reaction vessel.
  • the vapor from the preprocessing step can be processed separately or combined with the vapor phase product from the reaction vessel of the present invention.
  • the vapor phase product(s) may undergo further vapor phase hydroprocessing if greater reduction in heteroatom and aromatic species is desired or sent directly to a recovery system.
  • the countercurrent contacting of liquid and the treat gas in the contacting zone strips dissolved gaseous impurities, such as H 2 S and NH 3 from the effluent stream, thereby improving both the hydrogen partial pressure and the catalyst performance.
  • the resulting final liquid product will contain a substantially lower level of heteroatoms than the original feedstock.
  • This liquid product stream may be sent to downstream hydroprocessing or conversion processes.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
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US6623621B1 (en) * 1998-12-07 2003-09-23 Exxonmobil Research And Engineering Company Control of flooding in a countercurrent flow reactor by use of temperature of liquid product stream
WO2010117856A2 (en) * 2009-04-08 2010-10-14 Uop Llc Vapor-liquid contacting apparatuses with vortex contacting stages
EP2262585A1 (en) * 2008-02-27 2010-12-22 Kellogg Brown & Root LLC Split flow contactor
US8968552B2 (en) 2011-11-04 2015-03-03 Saudi Arabian Oil Company Hydrotreating and aromatic saturation process with integral intermediate hydrogen separation and purification
WO2015081395A1 (pt) * 2013-12-06 2015-06-11 Petróleo Brasileiro S.A. - Petrobras Reator em regime fluidodinâmico combinado para o tratamento do petróleo e seus derivados
US20160074824A1 (en) * 2011-09-22 2016-03-17 Donald Hugh McKinley Apparatus And Method For Heterogeneous Catalytic Reactions
CN108499493A (zh) * 2018-05-02 2018-09-07 西安纳瑞工控科技有限公司 一种气液逆流反应装置
CN109045947A (zh) * 2018-09-03 2018-12-21 青岛科技大学 一种流化床簇反应器

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US6623622B2 (en) * 2000-10-10 2003-09-23 Exxonmobil Research And Engineering Company Two stage diesel fuel hydrotreating and stripping in a single reaction vessel
US6632350B2 (en) * 2000-10-10 2003-10-14 Exxonmobile Research And Engineering Company Two stage hydroprocessing and stripping in a single reaction vessel
CN100434155C (zh) 2003-08-18 2008-11-19 国际壳牌研究有限公司 分配装置
CN102041069B (zh) * 2009-10-16 2013-12-04 中国石油化工股份有限公司 一种柴油脱硫、脱氮及芳烃饱和的气液逆流加氢方法
KR101669805B1 (ko) * 2016-07-15 2016-10-27 보성환경이엔텍 주식회사 탈취형 스크러버

Citations (73)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2952626A (en) 1957-08-05 1960-09-13 Union Oil Co Mixed-phase hydrofining of hydrocarbon oils
US2971754A (en) 1958-07-16 1961-02-14 Ohio Crankshaft Co Control of high frequency induction heating
US2987467A (en) 1958-05-26 1961-06-06 Hydrocarbon Research Inc Removal of sulfur and metals from heavy oils by hydro-catalytic treatment
US3017345A (en) 1960-07-12 1962-01-16 Texaco Inc Treatment of hydrocarbons
US3091586A (en) 1959-12-15 1963-05-28 Exxon Research Engineering Co Hydrofining of shale oil
US3124526A (en) 1964-03-10 Rhigh boiling
US3147210A (en) 1962-03-19 1964-09-01 Union Oil Co Two stage hydrogenation process
US3211641A (en) 1962-04-11 1965-10-12 Socony Mobil Oil Co Inc Gas-liquid reactions and apparatus therefor, for the hydrogenation and hydrocrackingof hydrocarbons
US3228871A (en) 1962-08-07 1966-01-11 Texaco Inc Treatment of hydrocarbons with hydrocracking in the first stage and hydrogenation ofthe gaseous products
US3268438A (en) 1965-04-29 1966-08-23 Chevron Res Hydrodenitrification of oil with countercurrent hydrogen
US3413216A (en) 1965-12-13 1968-11-26 Union Oil Co Process for selectively desulfurizing mercaptans
US3415737A (en) 1966-06-24 1968-12-10 Chevron Res Reforming a sulfur-free naphtha with a platinum-rhenium catalyst
US3425810A (en) 1965-05-03 1969-02-04 Chevron Res Hydrotreating apparatus
US3450784A (en) 1966-09-22 1969-06-17 Lummus Co Hydrogenation of benzene to cyclohexane
US3461063A (en) 1966-04-04 1969-08-12 Universal Oil Prod Co Hydrogenation process
US3595779A (en) 1969-03-28 1971-07-27 Texaco Inc Catalytic hydrogen contact process
US3607723A (en) 1969-03-28 1971-09-21 Texaco Inc Split flow hydrocracking process
US3658681A (en) 1970-02-24 1972-04-25 Texaco Inc Production of low sulfur fuel oil
US3671420A (en) 1970-12-24 1972-06-20 Texaco Inc Conversion of heavy petroleum oils
US3673078A (en) 1970-03-04 1972-06-27 Sun Oil Co Process for producing high ur oil by hydrogenation of dewaxed raffinate
US3714030A (en) 1967-07-11 1973-01-30 J Winsor Desulphurization and hydrogenation of aromatic-containing hydrocarbon fractions
GB1323257A (en) 1971-07-08 1973-07-11 Texaco Development Corp Catalytic hydrogen contact process
US3767562A (en) 1971-09-02 1973-10-23 Lummus Co Production of jet fuel
US3775291A (en) 1971-09-02 1973-11-27 Lummus Co Production of jet fuel
US3788976A (en) 1970-03-04 1974-01-29 Sun Oil Co Pennsylvania Multi-stage process for producing high ur oil by hydrogenation
US3843508A (en) 1970-12-24 1974-10-22 Texaco Inc Split flow hydrodesulfurization and catalytic cracking of residue-containing petroleum fraction
US3846278A (en) 1971-09-02 1974-11-05 Lummus Co Production of jet fuel
US3897329A (en) 1973-12-26 1975-07-29 Texaco Inc Spit flow hydrodesulfurization of petroleum fraction
US3905893A (en) 1973-08-22 1975-09-16 Gulf Research Development Co Plural stage residue hydrodesulfurization process
US4021330A (en) 1975-09-08 1977-05-03 Continental Oil Company Hydrotreating a high sulfur, aromatic liquid hydrocarbon
US4022682A (en) 1975-12-22 1977-05-10 Gulf Research & Development Company Hydrodenitrogenation of shale oil using two catalysts in series reactors
US4026674A (en) 1975-10-30 1977-05-31 Commonwealth Oil Refining Co., Inc. Multi-stage reactor
US4194964A (en) 1978-07-10 1980-03-25 Mobil Oil Corporation Catalytic conversion of hydrocarbons in reactor fractionator
US4212726A (en) 1977-11-23 1980-07-15 Cosden Technology, Inc. Method for increasing the purity of hydrogen recycle gas
US4213847A (en) 1979-05-16 1980-07-22 Mobil Oil Corporation Catalytic dewaxing of lubes in reactor fractionator
US4243519A (en) 1979-02-14 1981-01-06 Exxon Research & Engineering Co. Hydrorefining process
DE2935191A1 (de) 1979-08-31 1981-04-02 Metallgesellschaft Ag, 6000 Frankfurt Verfahren zur gewinnung von dieseloel
US4457834A (en) 1983-10-24 1984-07-03 Lummus Crest, Inc. Recovery of hydrogen
US4476069A (en) 1983-02-23 1984-10-09 The Dow Chemical Company Liquid distributing apparatus for a liquid-vapor contact column
US4526757A (en) 1982-11-01 1985-07-02 Exxon Research And Engineering Co. Pulsed flow vapor-liquid reactor
US4591426A (en) 1981-10-08 1986-05-27 Intevep, S.A. Process for hydroconversion and upgrading of heavy crudes of high metal and asphaltene content
US4599162A (en) 1984-12-21 1986-07-08 Mobil Oil Corporation Cascade hydrodewaxing process
US4624748A (en) 1984-06-29 1986-11-25 Chevron Research Company Catalyst system for use in a distillation column reactor
US4755281A (en) 1984-05-01 1988-07-05 Mobil Oil Corporation Countercurrent process with froth control for treating heavy hydrocarbons
US4801373A (en) 1986-03-18 1989-01-31 Exxon Research And Engineering Company Process oil manufacturing process
US4952306A (en) 1989-09-22 1990-08-28 Exxon Research And Engineering Company Slurry hydroprocessing process
US5026459A (en) 1988-03-21 1991-06-25 Institut Francais Du Petrole Apparatus for reactive distillation
US5082551A (en) 1988-08-25 1992-01-21 Chevron Research And Technology Company Hydroconversion effluent separation process
US5183556A (en) 1991-03-13 1993-02-02 Abb Lummus Crest Inc. Production of diesel fuel by hydrogenation of a diesel feed
US5252198A (en) 1989-05-10 1993-10-12 Davy Mckee (London) Ltd. Multi-step hydrodesulphurisation process
US5262044A (en) 1991-10-01 1993-11-16 Shell Oil Company Process for upgrading a hydrocarbonaceous feedstock and apparatus for use therein
US5292428A (en) 1989-05-10 1994-03-08 Davy Mckee (London) Ltd. Multi-step hydrodesulphurization process
RU2016617C1 (ru) 1991-06-25 1994-07-30 Московская государственная академия химического машиностроения Способ организации потоков в массообменных аппаратах
US5348641A (en) 1991-08-15 1994-09-20 Mobil Oil Corporation Gasoline upgrading process
US5366614A (en) 1989-09-18 1994-11-22 Uop Catalytic reforming process with sulfur preclusion
US5378348A (en) 1993-07-22 1995-01-03 Exxon Research And Engineering Company Distillate fuel production from Fischer-Tropsch wax
US5449501A (en) 1994-03-29 1995-09-12 Uop Apparatus and process for catalytic distillation
US5518607A (en) 1984-10-31 1996-05-21 Field; Leslie A. Sulfur removal systems for protection of reforming catalysts
US5522198A (en) 1995-04-20 1996-06-04 Byer; Gary M. Method of using a woven carbon fabric to protect houses, persons and other structures from flames and heat
US5522983A (en) 1992-02-06 1996-06-04 Chevron Research And Technology Company Hydrocarbon hydroconversion process
US5670116A (en) 1995-12-05 1997-09-23 Exxon Research & Engineering Company Hydroprocessing reactor with enhanced product selectivity
US5705052A (en) 1996-12-31 1998-01-06 Exxon Research And Engineering Company Multi-stage hydroprocessing in a single reaction vessel
US5720872A (en) 1996-12-31 1998-02-24 Exxon Research And Engineering Company Multi-stage hydroprocessing with multi-stage stripping in a single stripper vessel
US5779992A (en) 1993-08-18 1998-07-14 Catalysts & Chemicals Industries Co., Ltd. Process for hydrotreating heavy oil and hydrotreating apparatus
US5882505A (en) 1997-06-03 1999-03-16 Exxon Research And Engineering Company Conversion of fisher-tropsch waxes to lubricants by countercurrent processing
US5888377A (en) 1997-12-19 1999-03-30 Uop Llc Hydrocracking process startup method
US5888376A (en) 1996-08-23 1999-03-30 Exxon Research And Engineering Co. Conversion of fischer-tropsch light oil to jet fuel by countercurrent processing
US5906728A (en) 1996-08-23 1999-05-25 Exxon Chemical Patents Inc. Process for increased olefin yields from heavy feedstocks
US5925235A (en) 1997-12-22 1999-07-20 Chevron U.S.A. Inc. Middle distillate selective hydrocracking process
US5939031A (en) 1996-08-23 1999-08-17 Exxon Research And Engineering Co. Countercurrent reactor
US5942197A (en) 1996-08-23 1999-08-24 Exxon Research And Engineering Co Countercurrent reactor
US5985131A (en) 1996-08-23 1999-11-16 Exxon Research And Engineering Company Hydroprocessing in a countercurrent reaction vessel
US6007787A (en) 1996-08-23 1999-12-28 Exxon Research And Engineering Co. Countercurrent reaction vessel

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2981677A (en) * 1957-05-28 1961-04-25 Socony Mobil Oil Co Inc Conversion of liquid hydrocarbon in the presence of a gaseous reactant and particle-form solid catalytic material
US4604261A (en) * 1984-06-29 1986-08-05 Mobil Oil Corporation Hydroprocessing reactor for catalytically dewaxing liquid petroleum feedstocks
FR2743079B1 (fr) * 1995-12-27 1998-02-06 Inst Francais Du Petrole Procede et dispositif d'hydrogenation selective par distillation catalytique comportant une zone reactionnelle a co-courant ascendant liquide-gaz

Patent Citations (73)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3124526A (en) 1964-03-10 Rhigh boiling
US2952626A (en) 1957-08-05 1960-09-13 Union Oil Co Mixed-phase hydrofining of hydrocarbon oils
US2987467A (en) 1958-05-26 1961-06-06 Hydrocarbon Research Inc Removal of sulfur and metals from heavy oils by hydro-catalytic treatment
US2971754A (en) 1958-07-16 1961-02-14 Ohio Crankshaft Co Control of high frequency induction heating
US3091586A (en) 1959-12-15 1963-05-28 Exxon Research Engineering Co Hydrofining of shale oil
US3017345A (en) 1960-07-12 1962-01-16 Texaco Inc Treatment of hydrocarbons
US3147210A (en) 1962-03-19 1964-09-01 Union Oil Co Two stage hydrogenation process
US3211641A (en) 1962-04-11 1965-10-12 Socony Mobil Oil Co Inc Gas-liquid reactions and apparatus therefor, for the hydrogenation and hydrocrackingof hydrocarbons
US3228871A (en) 1962-08-07 1966-01-11 Texaco Inc Treatment of hydrocarbons with hydrocracking in the first stage and hydrogenation ofthe gaseous products
US3268438A (en) 1965-04-29 1966-08-23 Chevron Res Hydrodenitrification of oil with countercurrent hydrogen
US3425810A (en) 1965-05-03 1969-02-04 Chevron Res Hydrotreating apparatus
US3413216A (en) 1965-12-13 1968-11-26 Union Oil Co Process for selectively desulfurizing mercaptans
US3461063A (en) 1966-04-04 1969-08-12 Universal Oil Prod Co Hydrogenation process
US3415737A (en) 1966-06-24 1968-12-10 Chevron Res Reforming a sulfur-free naphtha with a platinum-rhenium catalyst
US3450784A (en) 1966-09-22 1969-06-17 Lummus Co Hydrogenation of benzene to cyclohexane
US3714030A (en) 1967-07-11 1973-01-30 J Winsor Desulphurization and hydrogenation of aromatic-containing hydrocarbon fractions
US3595779A (en) 1969-03-28 1971-07-27 Texaco Inc Catalytic hydrogen contact process
US3607723A (en) 1969-03-28 1971-09-21 Texaco Inc Split flow hydrocracking process
US3658681A (en) 1970-02-24 1972-04-25 Texaco Inc Production of low sulfur fuel oil
US3788976A (en) 1970-03-04 1974-01-29 Sun Oil Co Pennsylvania Multi-stage process for producing high ur oil by hydrogenation
US3673078A (en) 1970-03-04 1972-06-27 Sun Oil Co Process for producing high ur oil by hydrogenation of dewaxed raffinate
US3671420A (en) 1970-12-24 1972-06-20 Texaco Inc Conversion of heavy petroleum oils
US3843508A (en) 1970-12-24 1974-10-22 Texaco Inc Split flow hydrodesulfurization and catalytic cracking of residue-containing petroleum fraction
GB1323257A (en) 1971-07-08 1973-07-11 Texaco Development Corp Catalytic hydrogen contact process
US3767562A (en) 1971-09-02 1973-10-23 Lummus Co Production of jet fuel
US3775291A (en) 1971-09-02 1973-11-27 Lummus Co Production of jet fuel
US3846278A (en) 1971-09-02 1974-11-05 Lummus Co Production of jet fuel
US3905893A (en) 1973-08-22 1975-09-16 Gulf Research Development Co Plural stage residue hydrodesulfurization process
US3897329A (en) 1973-12-26 1975-07-29 Texaco Inc Spit flow hydrodesulfurization of petroleum fraction
US4021330A (en) 1975-09-08 1977-05-03 Continental Oil Company Hydrotreating a high sulfur, aromatic liquid hydrocarbon
US4026674A (en) 1975-10-30 1977-05-31 Commonwealth Oil Refining Co., Inc. Multi-stage reactor
US4022682A (en) 1975-12-22 1977-05-10 Gulf Research & Development Company Hydrodenitrogenation of shale oil using two catalysts in series reactors
US4212726A (en) 1977-11-23 1980-07-15 Cosden Technology, Inc. Method for increasing the purity of hydrogen recycle gas
US4194964A (en) 1978-07-10 1980-03-25 Mobil Oil Corporation Catalytic conversion of hydrocarbons in reactor fractionator
US4243519A (en) 1979-02-14 1981-01-06 Exxon Research & Engineering Co. Hydrorefining process
US4213847A (en) 1979-05-16 1980-07-22 Mobil Oil Corporation Catalytic dewaxing of lubes in reactor fractionator
DE2935191A1 (de) 1979-08-31 1981-04-02 Metallgesellschaft Ag, 6000 Frankfurt Verfahren zur gewinnung von dieseloel
US4591426A (en) 1981-10-08 1986-05-27 Intevep, S.A. Process for hydroconversion and upgrading of heavy crudes of high metal and asphaltene content
US4526757A (en) 1982-11-01 1985-07-02 Exxon Research And Engineering Co. Pulsed flow vapor-liquid reactor
US4476069A (en) 1983-02-23 1984-10-09 The Dow Chemical Company Liquid distributing apparatus for a liquid-vapor contact column
US4457834A (en) 1983-10-24 1984-07-03 Lummus Crest, Inc. Recovery of hydrogen
US4755281A (en) 1984-05-01 1988-07-05 Mobil Oil Corporation Countercurrent process with froth control for treating heavy hydrocarbons
US4624748A (en) 1984-06-29 1986-11-25 Chevron Research Company Catalyst system for use in a distillation column reactor
US5518607A (en) 1984-10-31 1996-05-21 Field; Leslie A. Sulfur removal systems for protection of reforming catalysts
US4599162A (en) 1984-12-21 1986-07-08 Mobil Oil Corporation Cascade hydrodewaxing process
US4801373A (en) 1986-03-18 1989-01-31 Exxon Research And Engineering Company Process oil manufacturing process
US5026459A (en) 1988-03-21 1991-06-25 Institut Francais Du Petrole Apparatus for reactive distillation
US5082551A (en) 1988-08-25 1992-01-21 Chevron Research And Technology Company Hydroconversion effluent separation process
US5252198A (en) 1989-05-10 1993-10-12 Davy Mckee (London) Ltd. Multi-step hydrodesulphurisation process
US5292428A (en) 1989-05-10 1994-03-08 Davy Mckee (London) Ltd. Multi-step hydrodesulphurization process
US5366614A (en) 1989-09-18 1994-11-22 Uop Catalytic reforming process with sulfur preclusion
US4952306A (en) 1989-09-22 1990-08-28 Exxon Research And Engineering Company Slurry hydroprocessing process
US5183556A (en) 1991-03-13 1993-02-02 Abb Lummus Crest Inc. Production of diesel fuel by hydrogenation of a diesel feed
RU2016617C1 (ru) 1991-06-25 1994-07-30 Московская государственная академия химического машиностроения Способ организации потоков в массообменных аппаратах
US5348641A (en) 1991-08-15 1994-09-20 Mobil Oil Corporation Gasoline upgrading process
US5262044A (en) 1991-10-01 1993-11-16 Shell Oil Company Process for upgrading a hydrocarbonaceous feedstock and apparatus for use therein
US5522983A (en) 1992-02-06 1996-06-04 Chevron Research And Technology Company Hydrocarbon hydroconversion process
US5378348A (en) 1993-07-22 1995-01-03 Exxon Research And Engineering Company Distillate fuel production from Fischer-Tropsch wax
US5779992A (en) 1993-08-18 1998-07-14 Catalysts & Chemicals Industries Co., Ltd. Process for hydrotreating heavy oil and hydrotreating apparatus
US5449501A (en) 1994-03-29 1995-09-12 Uop Apparatus and process for catalytic distillation
US5522198A (en) 1995-04-20 1996-06-04 Byer; Gary M. Method of using a woven carbon fabric to protect houses, persons and other structures from flames and heat
US5670116A (en) 1995-12-05 1997-09-23 Exxon Research & Engineering Company Hydroprocessing reactor with enhanced product selectivity
US5939031A (en) 1996-08-23 1999-08-17 Exxon Research And Engineering Co. Countercurrent reactor
US6007787A (en) 1996-08-23 1999-12-28 Exxon Research And Engineering Co. Countercurrent reaction vessel
US5985131A (en) 1996-08-23 1999-11-16 Exxon Research And Engineering Company Hydroprocessing in a countercurrent reaction vessel
US5942197A (en) 1996-08-23 1999-08-24 Exxon Research And Engineering Co Countercurrent reactor
US5888376A (en) 1996-08-23 1999-03-30 Exxon Research And Engineering Co. Conversion of fischer-tropsch light oil to jet fuel by countercurrent processing
US5906728A (en) 1996-08-23 1999-05-25 Exxon Chemical Patents Inc. Process for increased olefin yields from heavy feedstocks
US5705052A (en) 1996-12-31 1998-01-06 Exxon Research And Engineering Company Multi-stage hydroprocessing in a single reaction vessel
US5720872A (en) 1996-12-31 1998-02-24 Exxon Research And Engineering Company Multi-stage hydroprocessing with multi-stage stripping in a single stripper vessel
US5882505A (en) 1997-06-03 1999-03-16 Exxon Research And Engineering Company Conversion of fisher-tropsch waxes to lubricants by countercurrent processing
US5888377A (en) 1997-12-19 1999-03-30 Uop Llc Hydrocracking process startup method
US5925235A (en) 1997-12-22 1999-07-20 Chevron U.S.A. Inc. Middle distillate selective hydrocracking process

Cited By (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6623621B1 (en) * 1998-12-07 2003-09-23 Exxonmobil Research And Engineering Company Control of flooding in a countercurrent flow reactor by use of temperature of liquid product stream
EP2262585A4 (en) * 2008-02-27 2013-01-16 Kellogg Brown & Root Llc CONTACTOR WITH SEPARATE FLOW
EP2262585A1 (en) * 2008-02-27 2010-12-22 Kellogg Brown & Root LLC Split flow contactor
CN102802780B (zh) * 2009-04-08 2014-08-06 环球油品公司 具有涡流接触级的气-液接触设备
CN102802780A (zh) * 2009-04-08 2012-11-28 环球油品公司 具有涡流接触级的气-液接触设备
WO2010117856A3 (en) * 2009-04-08 2011-01-13 Uop Llc Vapor-liquid contacting apparatuses with vortex contacting stages
RU2482910C1 (ru) * 2009-04-08 2013-05-27 Юоп Ллк Аппараты для контактирования пара и жидкости, содержащие вихревые контактные ступени
KR101352676B1 (ko) 2009-04-08 2014-01-16 유오피 엘엘씨 와류 접촉단을 구비한 증기-액체 접촉 장치
WO2010117856A2 (en) * 2009-04-08 2010-10-14 Uop Llc Vapor-liquid contacting apparatuses with vortex contacting stages
US20160074824A1 (en) * 2011-09-22 2016-03-17 Donald Hugh McKinley Apparatus And Method For Heterogeneous Catalytic Reactions
US9539555B2 (en) * 2011-09-22 2017-01-10 Davy Process Technology Limited Apparatus and method for heterogeneous catalytic reactions
US8968552B2 (en) 2011-11-04 2015-03-03 Saudi Arabian Oil Company Hydrotreating and aromatic saturation process with integral intermediate hydrogen separation and purification
WO2015081395A1 (pt) * 2013-12-06 2015-06-11 Petróleo Brasileiro S.A. - Petrobras Reator em regime fluidodinâmico combinado para o tratamento do petróleo e seus derivados
CN108499493A (zh) * 2018-05-02 2018-09-07 西安纳瑞工控科技有限公司 一种气液逆流反应装置
CN108499493B (zh) * 2018-05-02 2024-05-14 西安纳瑞工控科技有限公司 一种气液逆流反应装置
CN109045947A (zh) * 2018-09-03 2018-12-21 青岛科技大学 一种流化床簇反应器

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